Customized MEE & ATFD Systems for Fine & Specialty Chemicals

Executive Engineering Summary: Fine and specialty chemical manufacturing plants generate complex, highly toxic effluent streams characterized by elevated Total Dissolved Solids (TDS), high Chemical Oxygen Demand (COD), variable organic solvent carryover, and aggressive corrosive species such as halide salts, organic acids, and aromatic sulfonates. Implementing a robust Zero Liquid Discharge (ZLD) framework requires specialized, customized Multi-Effect Evaporators (MEE) and Agitated Thin Film Dryers (ATFD) engineered to resist stress corrosion cracking, handle high boiling point elevation (BPE), and maintain continuous heat transfer under severe thermal fouling and viscous regimes.

1. Process Overview & ZLD Loop Integration

In fine chemical and Active Pharmaceutical Ingredient (API) intermediate manufacturing, process streams exhibit extreme batch-to-batch variability. Unlike municipal or basic chemical wastewater systems, fine chemical effluents contain a mixture of inorganic salts (e.g., NaCl, Na_2SO_4, NH_4Cl, CaCl_2) combined with complex organic salts (e.g., sodium acetate, sodium formate, phenolates, and substituted amine salts).

 Raw Chemical Effluent 
        │
        ▼
┌──────────────────────────┐
│ Pre-Treatment & Neutral  │ ──► High-COD Stripping / Solvent Recovery
└───────────┬──────────────┘
            │
            ▼
┌──────────────────────────┐
│ Membrane Concentration   │ ──► Permeate Stream (Reused in Cooling Towers)
│ (RO / High-Pressure RO)  │
└───────────┬──────────────┘
            │ Concentrated Reject (TDS: 6% - 12%)
            ▼
┌──────────────────────────┐      ┌──────────────────────────┐
│ Multi-Effect Evaporator  │ ───► │ Overhead Vapor Condenser │ ──► Recovered Distillate (TDS < 50 ppm)
│ (MEE + TVR / MVR Loop)   │      └──────────────────────────┘
└───────────┬──────────────┘
            │ Concentrated Slurry / Concentrate (TDS: 35% - 45%)
            ▼
┌──────────────────────────┐      ┌──────────────────────────┐
│ [Agitated Thin Film Dryer](/process/equipment/atfd) │ ───► │ ATFD Vapor Condenser     │ ──► Recycle to MEE Pre-heater
│ (ATFD Crystallization)   │      └──────────────────────────┘
└───────────┬──────────────┘
            │
            ▼
┌──────────────────────────┐
│ Powdered Solid Salt      │ ──► Hazardous Landfill / Salt Recovery
│ (Moisture < 3-5% w/w)    │
└──────────────────────────┘

The Core Challenge in Fine Chemicals ZLD Architecture

1. Solvent & Organic Contamination: Traces of toluene, methanol, dimethylformamide (DMF), or dichloromethane (DCM) lower the vapor temperature and create flammable vapor risks in overhead condensers, demanding hazardous area classification (ATEX / Class 1 Div 1 or 2).
2. Boiling Point Elevation (BPE): High salt and solute concentrations raise the boiling temperature of the liquid by $10^\circ\text{C}$ to over $35^\circ\text{C}$ above pure water at the same pressure, drastically reducing the net effective temperature driving force (Δ T_{eff}) across evaporator effects.
3. Corrosive Synergism: Combined high chloride content (>50,000 ppm) and low pH (< 3.0) at elevated operating temperatures ($80^\circ\text{C} - 130^\circ\text{C}$) rapidly destroy standard austenitic stainless steels like SS304L and SS316L via pitting, crevice corrosion, and Chloride Stress Corrosion Cracking (CSCC).

2. Batch vs. Continuous Evaporation Dynamics

Fine chemical production facilities frequently operate on campaign schedules. Choosing between batch, semi-continuous, or continuous thermal concentration modes fundamentally dictates process stability, thermal efficiency, and mechanical fatigue life.

2.1 Batch Evaporation Mode

Batch evaporation is preferred when campaign volumes are under $15\text{ m}^3/\text{day}$, feed compositions shift drastically between products, or when the liquor tends to polymerize or degrade under prolonged thermal residence.

• Transient Heat Transfer: As water is vaporized, liquid volume decreases while viscosity and TDS surge exponentially. The overall heat transfer coefficient U(t) degrades dynamically:

U(t) = U_0  ·  e^{-k_f  ·  t}

where U_0 is the initial clean overall heat transfer coefficient (W/m²·K) and k_f is the fouling rate constant (hr^{-1}).

• Boiling Point Elevation Drift: As concentration increases, the saturation temperature increases rapidly, requiring steam control valves to automatically ramp supply pressure/temperature to maintain boiling rates.
• Foaming Kinetics: Batch operations suffer from severe foaming during the initial rapid boiling phase due to residual surface-active organic impurities.

2.2 Continuous Evaporation Mode

Continuous operation is optimal for dedicated production lines with capacities exceeding $25 - 50\text{ m}^3/\text{day}$.

• Steady-State Thermal Equilibrium: Feed flow, vapor withdrawal, condensate removal, and concentrate bleed are continuously balanced using feedback loops tied to inline mass flowmeters and density transmitters.
• Cascading Concentration Profiles: In a 3-effect continuous MEE, Effect 1 concentrates the raw feed from $8%$ to $15%$ TDS, Effect 2 from $15%$ to $28%$ TDS, and Effect 3 (Forced Circulation) takes the brine to $42%$ TDS prior to ATFD transfer.
• Fouling Minimization: Operating at constant liquid velocities (v > 2.2 m/s in Forced Circulation tubes) delays boundary layer salt crystallization and scale deposition.

3. Materials of Construction & Corrosion Engineering

Selecting the appropriate metallurgy for MEE heat exchangers, vapor-liquid separators, and ATFD thermal shells is the single most critical decision determining capital expenditures (CAPEX) and long-term equipment survival.

Corrosion Resistance Index (PREN) vs Metallurgy
─────────────────────────────────────────────────────────────────────────────
SS304L           │ PREN ~ 19      (Unsuitable for Chlorides)
SS316L           │ PREN ~ 23-25   (Limited to < 500 ppm Cl⁻, pH > 6.0)
Duplex 2205      │ PREN ~ 35      (Excellent for Moderate Chlorides, < 25,000 ppm)
Super Duplex 2507│ PREN ~ 42-45   (High Strength, High Chloride, T < 100°C)
Hastelloy C-276  │ PREN ~ 68-70   (Severe Acidic Chlorides, High T, Organics)
Titanium Gr. 2   │ PREN > 70*     (Oxidizing Acid Chlorides; Fails in Reducing HCl)
─────────────────────────────────────────────────────────────────────────────
*Note: Titanium PREN equivalent calculated based on localized pitting performance in oxidizing halide media.

3.1 Metallurgical Breakdown & Suitability

1. Stainless Steel 304L / 316L

• Microstructure: Austenitic.
• Operational Limits: SS316L is acceptable only for mild, neutral pH effluents with chloride concentration < 500 ppm and operating temperatures below $60^\circ\text{C}$.
• Failure Modes: Severe Pitting, Crevice Corrosion under salt deposits, and catastrophic CSCC above $60^\circ\text{C}$ in chloride environments.

2. Duplex 2205 (UNS S31803 / S32205)

• Microstructure: Ferritic-Austenitic (50/50 dual phase).
• Operational Limits: Chloride concentration up to $30,000\text{ ppm}$ at temperatures up to $90^\circ\text{C}$; pH range $4.0 - 11.0$.
• Benefits: Double the yield strength of SS316L, exceptional resistance to stress corrosion cracking due to ferritic phase matrix. Highly cost-effective for MEE Effect 1 & 2 calandrias.

3. Hastelloy C-276 (UNS N10276)

• Composition: 57% Ni, 16% Cr, 16% Mo, 4% W, 2.5% Co, 5% Fe.
• Operational Limits: Unlimited chloride concentration, highly acidic environments (pH < 1.0), mixed wet chlorine, acetic acid, formic acid, and aromatic sulfonate salts up to $160^\circ\text{C}$.
• Benefits: Outstanding resistance to localized corrosion (pitting, crevice) and reducing/oxidizing chemical environments. Essential for final MEE effects, Forced Circulation vapor heads, and ATFD thermal shells handling fine chemical brines.

4. Titanium Grade 2 (UNS R50400) & Grade 5 (UNS R56400)

• Microstructure: Unalloyed commercially pure α-Titanium (Grade 2).
• Operational Limits: Superior performance in oxidizing chloride environments (e.g., wet chlorine, bleach, ferric chloride).
• Caution: Highly vulnerable to severe rapid corrosion in reducing acids like pure hydrochloric acid (HCl) or hydrofluoric acid (HF) unless trace oxidizers or inhibitors are present.

5. Monel 400 (UNS N04400)

• Composition: 67% Ni, 30% Cu.
• Operational Limits: Excellent resistance to non-oxidizing chloride solutions, hydrofluoric acid, and strong caustic (NaOH) solutions. Unsuitable for oxidizing acid salts (e.g., nitric acid, ferric salts).

4. Mechanical & Process Design Parameters (ASME / TEMA / API)

Customized MEE and ATFD units for hazardous fine chemical processing must strictly adhere to international engineering standards to ensure structural integrity and pressure envelope compliance.

4.1 Applicable Engineering Codes

• ASME Section VIII, Division 1: Code for Design, Fabrication, and Inspection of Pressure Vessels (Evaporator Shells, Vapor Separators, ATFD Jackets).
• TEMA Class R & Class C: Tubular Exchanger Manufacturers Association standards for Shell & Tube Heat Exchanger calandrias.
• API 650: Welded Tanks for Oil/Chemical Liquid Storage (Feed and Distillate Balance Tanks).
• API 2000: Venting Atmospheric and Low-Pressure Storage Tanks (Overhead Condenser Vents, Emergency Relief).
• DIN EN 13445 / IS 2825: Unfired Pressure Vessel Design standards.

4.2 ATFD Rotor Mechanical & Seal Engineering

The Agitated Thin Film Dryer (ATFD) is the most mechanically demanding equipment in the ZLD loop. It converts concentrated slurry ($35 - 45%\text{ TDS}$) into dry solid salt (< 3-5% moisture) via mechanical film agitation.

       ATFD CROSS-SECTIONAL MECHANICAL SCHEMATIC
       ─────────────────────────────────────────
                Motor & Gearbox Drive
                        │
                  Upper Bearing
                        │
                Double Mechanical Seal (Plan 53A / Thermosiphon)
  Vapor Out ◄───┌────────────────┐
                │  Rotor Shaft   │
  Steam In ───► │ ┌────────────┐ │
                │ │  Hinged    │ │ ◄── Shell Inner Wall (Hastelloy C-276 / Duplex 2205)
  Product Feed► │ │ Scraper    │ │
                │ │ Blades     │ │ ◄── Heating Jacket (SS304L / Carbon Steel)
                │ └────────────┘ │
                │   Agitated     │
                │  Thin Film     │
                └────────────────┘
                        │
                  Bottom Steady Bearing (Self-lubricated PTFE/Graphite)
                        │
               Powder Discharge Flange (Zero Leak Vane Valve)

Key ATFD Mechanical Components:

1. Rotor Blade Configuration:
   • Hinged Scraper Blades: Flexible PTFE, Carbon-Graphite, or Hastelloy C-276 blades hinged to rotor arms. Centrifugal force pushes the blades against the inner thermal wall, sweeping away scaling crust and scraping dried powder without mechanical binding.
   • Fixed Clearance Blades: Fixed metallic wipers set at a tight radial gap ($0.75\text{ mm} - 1.5\text{ mm}$) relative to the inner shell, used for highly abrasive crystalline salts.
2. Dynamic Balancing: Rotor assemblies must undergo dynamic balancing per ISO 1940-1 Grade G2.5 to prevent low-frequency structural vibration and wall clearance degradation at operating speeds ($100 - 300\text{ RPM}$, corresponding to tip speeds of $8.5 - 12.5\text{ m/s}$).
3. Shaft Sealing Systems:
   • Double Mechanical Seals with API Plan 53A or Plan 53B Thermosiphon barrier fluid systems (polyethylene glycol or synthetic oil barrier fluid pressurized at $1.5 - 2.0\text{ bar}$ above vessel operating pressure).
   • Prevents toxic organic solvent vapors from leaking to atmosphere and guards against particulate salt ingress into seal faces.

5. Thermodynamic Modeling, Mass Balance & Sizing Logic

Designing an energy-optimized MEE and ATFD system requires solving coupled non-linear mass, heat, and Phase Equilibrium equations.

              MEE & ATFD MASS & HEAT BALANCE SCHEMATIC
              ────────────────────────────────────────
                      Vapor V1           Vapor V2          Vapor V3
                         │                  │                 │
    Steam (S0) ──────► ┌───┐             ┌───┐             ┌───┐
                       │E1 │             │E2 │             │E3 │ ──► Concentrate
    Feed (F, xF) ────► └───┘ ──────────► └───┘ ──────────► └───┘        (L3, x3)
                         │                  │                 │            │
                    Condensate C1      Condensate C2     Condensate C3     │
                                                                           ▼
                                                                     ┌───────────┐
                                                                     │   ATFD    │ ──► Vapor V_ATFD
                                                                     └─────┬─────┘
                                                                           │
                                                                           ▼
                                                                     Solid Salt (P, xP)

5.1 Boiling Point Elevation (BPE) & Activity Models

For multicomponent fine chemical streams containing organic salts and inorganic halides, the saturated vapor pressure of water is suppressed, resulting in significant Boiling Point Elevation (Δ T_{BPE}):

Δ T_{BPE} = T_{solution}(P, \mathbf{x}) - T_{water, sat}(P)

Using the modified Dühring's rule or NRTL (Non-Random Two-Liquid) thermodynamic model:

\ln a_w = \ln(\gamma_w  ·  x_w) = -(M_w) / (1000) Σ_{i} \nu_i m_i φ

where:

• a_w = activity of water in the brine mixture
• \gamma_w = activity coefficient of water
• x_w = mole fraction of water
• M_w = molecular weight of water ($18.015\text{ g/mol}$)
• m_i = molality of solute species i
• φ = osmotic coefficient of the mixture

5.2 Multi-Effect Mass and Energy Balances

Total Mass Balance:

F = Σ_{i=1}^n V_i + V_{ATFD} + P

Solute Component Mass Balance:

F  ·  x_F = P  ·  x_P

where F is feed mass rate (kg/h), x_F is mass fraction of solids in feed, V_i is vapor evaporated in Effect i, P is powder product output rate, and x_P is solid content in powder (≈ 0.96 - 0.97).

Energy Balance across Effect i:

S_{i-1}  ·  \lambda_{s, i-1} = L_i  ·  C_{p, i}  ·  (T_{b, i} - T_{L, i-1}) + V_i  ·  \lambda_{v, i} + Q_{loss}

where:

• S_{i-1} = heating vapor entering Effect i (for Effect 1, S_0 is live steam rate)
• \lambda_{s, i-1} = latent heat of vaporization of supply steam (kJ/kg)
• L_i = liquid flow leaving Effect i (kg/h)
• C_{p, i} = specific heat capacity of liquid liquor (kJ/kg·K)
• T_{b, i} = boiling temperature of liquor in Effect i (^\circC)
• \lambda_{v, i} = latent heat of vapor generated in Effect i (kJ/kg)

5.3 Heat Transfer Area Sizing Equations

The required effective heat transfer area A_i for Effect i calandria is:

A_i = (Q_i) / (U_i  ·  Δ T_{eff), i}

The net available effective temperature difference Δ T_{eff, i} is calculated by subtracting system losses from the total available thermal head:

Δ T_{eff, i} = (T_{steam, i} - T_{sat, vapor, i}) - Δ T_{BPE, i} - Δ T_{hydrostatic} - Δ T_{loss}

Where:

• T_{steam, i} = temperature of driving steam/vapor to Effect i
• T_{sat, vapor, i} = saturation temperature of vapor at vessel operating pressure
• Δ T_{hydrostatic} = temperature increase due to liquid static head above heat transfer surface
• Δ T_{loss} = duct friction loss and entrainment separator pressure drop temperature reduction

Typical Design Heat Transfer Coefficients (U Values):

• Falling Film Evaporator (Low TDS < 15%): U = 1,400 - 2,200 W/m²·K
• Forced Circulation Evaporator (High TDS $25 - 45%$): U = 800 - 1,300 W/m²·K
• Agitated Thin Film Dryer (ATFD, Concentrate to Powder): U = 350 - 650 W/m²·K

5.4 ATFD Thermal & Mechanical Sizing Equations

The required thermal drying area A_{ATFD} is calculated by:

A_{ATFD} = (m_{evap, ATFD}  ·  \lambda_{v} + m_{feed, ATFD}  ·  C_p  ·  (T_{boiling} - T_{feed, ATFD})) / (U_{ATFD)  ·  (T_{jacket, steam} - T_{product, boiling})}

The motor drive power requirement for the ATFD rotor assembly accounts for film shearing viscous dissipation:

P_{motor} = (2 π  ·  N  ·  T_{rotor}) / (60  ·  η_{gear)}

T_{rotor} = 2 π  ·  R²  ·  L  ·  μ  ·  ((\omega  ·  R) / (\delta)) + T_{blade scraping}

where:

• N = rotor rotational speed (RPM)
• R = inner vessel radius (m)
• L = heated shell length (m)
• μ = dynamic viscosity of concentrated sludge (Pa·s)
• \delta = liquid film thickness (\sim 0.5 - 1.5 mm)
• T_{blade scraping} = mechanical torque contribution from hinged blade scraping force against wall crust
• η_{gear} = gearbox mechanical efficiency (≈ 0.92 - 0.95)

6. Comparative Selection Matrices

Table 1: Evaporation & Drying Technology Selection Matrix

Table 2: Metallurgical Compatibility Matrix against Fine Chemical Contaminants

7. Energy Optimization & Utility Reduction Strategies

Operating thermal ZLD systems is energy-intensive. Standard single-effect thermal evaporation consumes ≈ 650 kWh equivalent of thermal energy per cubic meter of water evaporated. Fine chemical plants utilize advanced thermal integration techniques to drop OPEX by up to 75%.

      ENERGY OPTIMIZATION INTEGRATION SCHEMATIC
      ─────────────────────────────────────────
                        Low-Pressure Driving Steam
                                    │
                                    ▼
                          ┌──────────────────┐
                          │ Thermo-Compressor│ ◄── High-Pressure Motive Steam
                          │     (TVR)        │
                          └────────┬─────────┘
                                   │
                                   ▼
  Raw Effluent ──► ┌───────────────────────────────┐
  Feed             │  Effect 1 Calandria (FFE)    │
  Pre-heated       └───────────────┬───────────────┘
                                   │ Condensate Heat Exchanger
                                   ▼
                   ┌───────────────────────────────┐
                   │  Effect 2 Calandria (FFE)    │
                   └───────────────┬───────────────┘
                                   │
                                   ▼
                   ┌───────────────────────────────┐
                   │ Effect 3 Forced Circulation   │
                   └───────────────┬───────────────┘
                                   │ Concentrated Slurry
                                   ▼
                   ┌───────────────────────────────┐
                   │ ATFD Solid Crystallizer       │ ◄── Recycled Overhead Vapor to Feed Heater
                   └───────────────────────────────┘

7.1 Thermal Vapor Recompression (TVR)

A Thermo-compressor (TVR) uses high-pressure motive steam ($6 - 16\text{ bar(g)}$) through a convergent-divergent ejector nozzle to entrain a fraction of lower-pressure vapor generated in Effect 1. The mixture is compressed to an intermediate pressure and recycled back into Effect 1 calandria as driving steam.

• Benefit: Increases overall steam economy of a 3-effect system from \sim 2.7 to $3.6 - 4.1\text{ kg water evaporated / kg live steam}$.

7.2 Mechanical Vapor Recompression (MVR) Integration

In locations with high steam costs and competitive electricity tariffs, Mechanical Vapor Recompression (MVR) replaces live steam completely during steady-state operation.

• Operating Principle: A high-efficiency centrifugal fan or roots blower compresses the overhead vapor from a single effect vessel, elevating its saturation pressure and temperature by $6^\circ\text{C} - 14^\circ\text{C}$. This compressed vapor is recycled into the same vessel's heating shell as the primary thermal utility.
• Specific Energy Consumption: Drops thermal energy consumption to zero, consuming only $18 - 28\text{ kWh/m}^3$ of electrical energy for compressor motor operation.

7.3 ATFD Overhead Vapor Integration

Vapor generated inside the ATFD is typically at $80^\circ\text{C} - 95^\circ\text{C}$ under slight vacuum. Instead of condensing this vapor in a dedicated utility-cooled heat exchanger, SEMCO routes the ATFD overhead vapor through an shell-and-tube heat exchanger to pre-heat cold incoming effluent feed entering Effect 1 of the MEE.

• Utility Saving: Cuts cooling water load by $12 - 18%$ and reduces live steam consumption in raw feed pre-heaters.

8. Real-World Engineering Case Study

High-TDS Agrochemical & Fine Intermediates Plant ZLD Implementation

1. Facility & Feed Characterization

A specialty agrochemical intermediates facility produced $50\text{ m}^3/\text{day}$ ($2.08\text{ m}^3/\text{h}$) of hazardous effluent containing high organic acids, sodium formate, sodium chloride, and dissolved aromatic intermediates.

• Feed Flow Rate: $2,083\text{ kg/h}$
• Total Dissolved Solids (TDS): $11.5\text{ wt}% \quad (239.5\text{ kg/h solids})$
• Chemical Oxygen Demand (COD): $24,500\text{ mg/L}$
• Chloride Content (Cl^-): $42,000\text{ ppm}$
• Operating pH: $3.2 - 3.8$
• Boiling Point Elevation (Δ T_{BPE} at $40%\text{ TDS}$): $14.2^\circ\text{C}$

       MASS BALANCE FLOW SHEET (CASE STUDY)
       ───────────────────────────────────
 Feed: 2,083 kg/h (11.5% TDS)
   │
   ▼
┌────────────────────────────────────────────────────────┐
│ 3-Effect MEE (Hastelloy C-276 / Duplex 2205 + TVR)     │ ──► Pure Distillate: 1,480 kg/h
└──────────────────────────┬─────────────────────────────┘     (TDS < 30 ppm, COD < 80 ppm)
                           │
                           ▼ Concentrated Slurry: 603 kg/h (39.7% TDS)
┌────────────────────────────────────────────────────────┐
│ ATFD System (Hastelloy C-276 Shell, Scraper Blades)    │ ──► ATFD Condensate: 354 kg/h
└──────────────────────────┬─────────────────────────────┘
                           │
                           ▼
                 Dry Solid Salt Output: 249 kg/h
                 (Moisture: 3.8% w/w)

2. Equipment Specifications & Metallurgy Selected

• Pre-heaters: Spiral Heat Exchanger in Duplex 2205.
• Effect 1 & 2 Evaporators (Falling Film): Tubes & Tube-sheets in Duplex 2205 (UNS S31803), Shell in SS316L.
• Effect 3 Evaporator (Forced Circulation): Tube bundle, vapor-liquid separator, and axial flow pump casing completely fabricated in Hastelloy C-276 (UNS N10276) to handle $40%\text{ TDS}$ brine containing $150,000\text{ ppm}$ chlorides at $85^\circ\text{C}$.
• Agitated Thin Film Dryer (ATFD): Inner thermal shell in Hastelloy C-276 clad plate ($6\text{ mm}$ Hastelloy C-276 + $16\text{ mm}$ carbon steel jacket); Hinged scraper blades in Carbon-reinforced PTFE; Double Mechanical Seal with API Plan 53A Thermosiphon unit.

3. Measured Performance & Operational Data

9. Conclusion & Engineering Best Practices

Customizing MEE and ATFD systems for fine chemical zero liquid discharge loops requires balancing thermal efficiency against mechanical reliability and metallurgical survival.

Checklist for Process & Project Engineers:

1. Never Assume Static Water Properties: Always run rigorous thermodynamic BPE regressions and activity coefficient calculations incorporating organic solute-salt interaction parameters.
2. Strictly Enforce Metallurgy Thresholds: Do not use SS316L for final effect forced circulation units or ATFD shells when chloride levels exceed $10,000\text{ ppm}$ at temperatures above $70^\circ\text{C}$. Specify Duplex 2205 as a baseline and Hastelloy C-276 for severe acidic/chloride duties.
3. Incorporate Forced Circulation Fluid Velocities: Maintain minimum tube velocities of $2.2 - 3.2\text{ m/s}$ in high-TDS effects to prevent premature boiling inside heat exchanger tubes.
4. Mechanical Seal Protection: Always fit ATFD systems with double mechanical seals backed by API Plan 53A/53B pressurized barrier fluid loops to prevent toxic solvent vapor escapes and seal face destruction by salt crystals.
5. Recover Waste Heat: Integrate ATFD overhead vapors into raw feed pre-heaters and utilize Thermo-Compressors (TVR) or MVR compressors to minimize steam and utility footprints.

For customized MEE & ATFD system sizing, corrosion auditing, and pilot testing for fine chemical effluents, contact the SEMCO Process Engineering Team.